CN111116288B - Method for producing propylene and ethylene - Google Patents
Method for producing propylene and ethylene Download PDFInfo
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- CN111116288B CN111116288B CN201811275261.9A CN201811275261A CN111116288B CN 111116288 B CN111116288 B CN 111116288B CN 201811275261 A CN201811275261 A CN 201811275261A CN 111116288 B CN111116288 B CN 111116288B
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
- C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
- C07C4/06—Catalytic processes
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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Abstract
The application relates to a method for producing propylene and ethylene, which comprises the steps of feeding a hydrocarbon stream into an olefin cracking unit to react to obtain an ethylene-propylene-containing stream and an unreacted hydrocarbon stream, feeding the unreacted hydrocarbon stream into an olefin superposition unit, and generating C by the olefin superposition unit 8 + The technical scheme of recycling all or part of components back to the olefin cracking unit has the characteristics of small circulation, low energy consumption, good economy and the like, and is particularly suitable for raw materials with lower olefin concentration.
Description
Technical Field
The application relates to a method for producing propylene and ethylene, in particular to a method for producing propylene and ethylene by using a catalytic method.
Background
The olefin catalytic cracking technology is a method for obtaining light molecular olefin propylene and ethylene by using various mixed C4-C6 as raw materials and catalytically cracking the olefin contained in the raw materials usually in the presence of a molecular sieve catalyst. Several olefin catalytic cracking processes, which are representative at present, mainly comprise: the Propylur process, the OCP process, the Omega process, the OCC process, and the Superflex process. The Propylur process is developed by Lurgi company of Germany, adopts a fixed bed reaction process, adopts steam as a dilution raw material, adopts a molecular sieve catalyst, and performs the reaction adiabatically at 500 ℃ and 0-0.1 MPaG, wherein the reactor is in a fixed bed type, and the reactor is prepared at two times; the ratio of steam to raw material is 0.5-3.0, and the service life of the catalyst reaches 15 months. The olefin conversion of the Propylur process reached 85%, the single pass propylene yield 40mol%, the ethylene yield 10mol% (relative to the total amount of olefins in the feed); the process has an exemplary set of equipment in Worringen, germany, and no industrial equipment is currently constructed. The OCP process is developed by the cooperation of UOP and Atofina, and a fixed bed reaction process is adopted, wherein the reaction is carried out at 500-600 ℃ and 0.1-0.4 MPaG; adopts a reaction system with high space velocity and no diluent gas. The Omega process was developed by the Asahi chemical company of Japan, the reaction was carried out in a single-stage, adiabatic fixed bed, and the catalyst was regenerated by switching between two reactors; the molecular sieve catalyst is adopted, the reaction is carried out under the conditions of 530-600 ℃ and 0-0.5 MPaG, the reaction space velocity WHSV is 3-10 h < -1 >, and the conversion rate of the olefin in the process is more than 75%. A set of apparatus for producing propylene by Omega method was established in water island at 6 th month in 2006 by Asahi chemical industry. The OCC process was developed by Shanghai petrochemical institute and the reaction was carried out adiabatically in a fixed bed. The process without dilution gas is adopted, the reaction space velocity WHSV is 15-30 h < -1 >, the reaction pressure is 0-0.15 MPaG, the reaction temperature is 500-560 ℃, and the single pass conversion rate of olefin is more than 65%. The OCC process was built at 2004 in the early Shanghai petrochemical company limited to pilot plant of 100 tons/year scale. In 2009, an OCC industrial plant of 6 ten thousand tons/year was built in the chinese petrochemical company.
Olefin polymerization is a process for the non-selective polymerization of C8 olefins over a catalyst using mixed hydrocarbons, particularly C4 olefins in a mixed C4 feedstock. The Olihed process is developed by the China petrochemical Shanghai petrochemical institute, the reaction is carried out in a tubular reactor, a solid phosphoric acid catalyst is adopted, the reaction is carried out at 160-220 ℃, and the reaction space velocity WHSV is 1.5-3.0 h < -1 >. Lanzhou petrochemical industry has been used in 2004 in a carbon tetraoligomerization plant using this process and Shanghai institute T-99 catalyst. The light four-carbon and heavy four-carbon raw materials are respectively used, and the average conversion rate of olefin is more than 81 percent.
Disclosure of Invention
The technical problem to be solved by the application is that the economic benefit of hydrocarbon stream treatment in the prior art is poor, especially the economic benefit of hydrocarbon stream treatment with low olefin concentration is poor; the problems that the separation of olefin components and alkane components in hydrocarbon streams is difficult (separation can only be performed through extraction), the economic benefit of the separation process is poor, and the like exist. The new method for producing ethylene propylene is provided, compared with the traditional method, the method can greatly reduce the circulating materials and greatly improve the economic benefit on the premise of reaching the same yield, and is especially suitable for materials with low olefin concentration.
Materials with lower concentrations, such as carbon four in refinery units, are treated industrially using olefin cracking technology, and to achieve higher overall conversion, unreacted feedstock is often recycled to the olefin cracking unit for treatment. Because the boiling points of the alkene and the alkane in the unreacted materials are relatively close (such as n-butane and 2-butene), a large amount of alkane which does not participate in the reaction returns to the reactor along with the alkene, so that the reaction system is supported too large, and the energy consumption is greatly increased.
The industrialized olefin superposition technology is mainly used for oil refining enterprises, and as the generated product is olefin, along with the upgrading of the quality of oil products, the product is often subjected to further hydrogenation to be blended into a gasoline pool, so that the product does not dominate the competition with a direct alkylation route. Under the large background of chemical transformation of oil refining enterprises, blending light hydrocarbon which can be used in chemical industry into a gasoline pool is also a waste of resources. According to one embodiment of the present application, a process for producing propylene and ethylene comprises the steps of: (1) Feeding the hydrocarbon stream into an olefin cracking unit for reaction to obtain an ethylene-propylene-containing stream and an unreacted hydrocarbon stream; (2) Feeding said unreacted hydrocarbon stream to an olefin polymerization unit; (3) C produced by olefin laminating unit 8 + The components are recycled to the olefin cracking unit in whole or in part; the hydrocarbon stream comprises a hydrocarbon selected from C 4 ～C 8 At least one of the olefins.
In the technical scheme of the application, the C generated by superposition 8 + The components are defined as: hydrocarbon material with carbon number not less than 8.
The process according to any one of the preceding or following embodiments, characterized in that C produced by the olefin folding unit 8 + At least 0.1% recycled to the olefin cracking unit; preferably at least 30% is recycled back to the olefin cracking unit; more preferably at least 70% is recycled back to the olefin cracking unit; most preferably at least 90% is recycled to the olefin cracking unit.
In the above embodiment, preferably, at least 30% of the unreacted hydrocarbon stream in step (2) is fed to the olefin polymerization unit, preferably at least 60%, more preferably at least 100%.
The process of any of the preceding or following embodiments, characterized in that the olefin content is not more than 70% by weight of the hydrocarbon stream; preferably not more than 60%; more preferably not more than 50%.
The process according to any of the preceding or following embodiments, characterized in that at least the cracking of olefins into propylene and ethylene takes place in the olefin cracking unit.
The process according to any of the preceding or following embodiments, characterized in that at least olefin oligomerization takes place in the olefin folding unit.
The process according to any of the preceding or following embodiments, characterized in that the catalyst employed in the olefin cracking unit comprises a molecular sieve based catalyst; preferably ZSM-5 molecular sieve.
The process according to any of the preceding or following embodiments, characterized in that the catalyst employed in the olefin folding unit is an acidic catalyst; preferably a solid phosphoric acid-based catalyst or a silica-alumina pellet-based catalyst.
The process according to any one of the preceding or following embodiments, characterized in that the hydrocarbon stream comprises a catalyst selected from C 4 ～C 6 At least one of the olefins; preferably the hydrocarbon stream contains a catalyst selected from C 4 ～C 5 At least one of the olefins; more preferably the hydrocarbon stream contains C 4 An olefin.
The process according to any one of the preceding or following embodiments, characterized in that in step (2) the hydrocarbon stream is fed to an olefin folding unit, resulting in an olefin-rich stream produced after olefin folding and an alkane-rich stream remaining after folding; the separation of the two streams is achieved by conventional separation.
Technical effects
By adopting the technical scheme of the application, through the combined process of the olefin cracking unit and the olefin folding unit, unreacted olefin is folded by the olefin folding unit to be changed into C with high conversion rate 8 + The components can be easily separated from alkane which does not participate in the reaction, so that the alkane is prevented from being recycled to the olefin cracking reactor, the scale and the energy consumption of the device can be greatly reduced, and a good technical effect is achieved.
According to the method for producing propylene and ethylene of the present application, in one embodiment, the feed amount of the catalytic cracking reactor can be reduced, so that the energy consumption of the olefin cracking unit can be reduced by more than 60%, and since the olefin polymerization reaction is exothermic, the energy consumption of the upper polymerization reaction is not high, and thus the energy consumption of the upper polymerization reaction is considered, the whole process flow is reduced by more than 30%, and the yields of propylene and ethylene can be kept substantially unchanged.
According to the method for producing propylene and ethylene of the present application, in one embodiment, the feed rate of the catalytic cracking reactor can be reduced by at most 70% on the premise that the yield of ethylene and propylene is substantially unchanged, compared with the prior art.
Drawings
FIG. 1 is a schematic process flow diagram of a preferred embodiment of the present application.
I is an olefin cracking unit;
II is an olefin superposition unit;
1 is a hydrocarbon stream feed;
2 is an ethylene-propylene containing stream produced by an olefin cracking unit;
3 is unreacted hydrocarbon stream feed;
4 is an olefin-rich stream produced after olefin polymerization;
5 is a material flow returned to the olefin cracking unit after olefin is overlapped;
6 is an alkane-rich material flow discharged after olefin is overlapped;
7 is the residual alkane-rich material flow after superposition;
feeding the hydrocarbon stream 1 into unit I for olefin cracking reaction to obtain stream 2, feeding the rest stream 3 into unit II to obtain stream 4 (i.e. C generated by olefin superposition unit) 8 + Component) and stream 7. A portion of stream 5 of stream 4 is returned to the unit I for continued cracking to produce ethylene propylene and stream 6 is vented out of the boundary zone.
Fig. 2 is a schematic process flow diagram of a conventional method.
I is an olefin cracking unit;
1 is a hydrocarbon stream feed;
2 is an ethylene-propylene containing stream produced by an olefin cracking unit;
3 is unreacted hydrocarbon stream feed;
8 is unreacted material (discharge boundary zone);
9 is unreacted material (recycled to the olefin cracking unit);
hydrocarbon stream 1 is fed to unit I and an olefin cracking reaction occurs to produce stream 2, the remainder stream 3, and a portion 9 of 3 is returned to the olefin cracking unit and stream 8 is vented to the boundary zone.
Detailed Description
The following detailed description of embodiments of the application is provided, but it should be noted that the scope of the application is not limited by these embodiments, but is defined by the appended claims.
All publications, patent applications, patents, and other references mentioned in this specification are herein incorporated by reference in their entirety. Unless defined otherwise, all technical and scientific terms used herein have the meaning commonly understood by one of ordinary skill in the art. In case of conflict, the present specification, definitions, will control.
When the specification derives materials, substances, methods, steps, devices, or elements and the like in the word "known to those skilled in the art", "prior art", or the like, such derived objects encompass those conventionally used in the art as the application suggests, but also include those which are not currently commonly used but which would become known in the art to be suitable for similar purposes.
In the context of the present application, the term "C4 olefin" refers to a mono-olefin having four carbon atoms. For example, as the C4 olefin, various isomers of butene such as 1-n-butene, 2-n-butene, and isobutene are contemplated.
In the context of the present application, the terms "C4-C8-olefins" and "C 4 -C 8 Olefins "are identical and refer to C4 olefins, C5 olefins, C6 olefins, C7 olefins, and C8 olefins.
Unless explicitly indicated, all percentages, parts, ratios, etc. mentioned in this specification are by weight unless otherwise clear to the routine knowledge of a person skilled in the art.
Any two or more embodiments of the application may be combined in any desired manner within the context of this specification, and the resulting solution is part of the original disclosure of this specification, while still falling within the scope of the application.
[ example 1 ]
The procedure shown in fig. 1 was used:
stream 1 contains 40% C4 olefins, 4% C5 olefins, 3% C6 olefins, 2% C7 olefins, 1% C8 olefins, 50% C4 paraffins, with a total flow of 1000kg/h.
Stream 3 produced in I (having a flow rate of 731kg/h and a C4-C8 olefin content of 231 kg/h) is fed to II and stream 4 produced in II (having a flow rate of 208kg/h and an olefin content of greater than 95%) is fed back to I.
The stream 2 obtained in I contains 87 kg/h of ethylene and 270g/h of propylene, the ethylene-propylene yield being 71.4% based on the effective feed (olefin) in stream 1.
The reaction materials entering I were stream 1 and stream 5, wherein stream 1 was 1000kg/h, stream 5 was 208kg/h, and the total amount was 1208kg/h.
[ example 2 ]
The procedure shown in fig. 1 was used:
stream 1 contains 40% C4 olefins, 4% C5 olefins, 3% C6 olefins, 2% C7 olefins, 1% C8 olefins, 50% C4 paraffins, with a total flow of 1000kg/h.
Stream 3 produced in I (at a flow rate of 730kg/h and a C4-C8 olefin content of 230 kg/h) was fed to II, and 90% of stream 4 produced in II (at a flow rate of 207kg/h and an olefin content of greater than 95%) was returned to I.
The stream 2 obtained in I contains 85kg/h of ethylene and 259g/h of propylene, the ethylene-propylene yield being 68.8% based on the effective feed (olefin) in stream 1.
The reaction materials entering I were stream 1 and stream 5, wherein stream 1 was 1000kg/h, stream 5 was 186kg/h and the total amount was 1186kg/h.
[ example 3 ]
The procedure shown in fig. 1 was used:
stream 1 contains 40% C4 olefins, 4% C5 olefins, 3% C6 olefins, 2% C7 olefins, 1% C8 olefins, 50% C4 paraffins, with a total flow of 1000kg/h.
Stream 3 produced in I (at a flow rate of 729kg/h and a C4-C8 olefin content of 229 kg/h) was fed to II, and stream 4 produced in II (at a flow rate of 205kg/h and an olefin content of more than 95%) was returned to I at 70%.
The stream 2 obtained in I contains 78 kg/h of ethylene, 237g/h of propylene and the yield of ethylene and propylene based on the effective feed (olefin) in stream 1 is 63%.
The reaction materials entering I were stream 1 and stream 5, wherein stream 1 was 1000kg/h, stream 5 was 144kg/h, and the total amount was 1144kg/h.
[ example 4 ]
The procedure shown in fig. 1 was used:
stream 1 contains 40% C4 olefins, 4% C5 olefins, 3% C6 olefins, 2% C7 olefins, 1% C8 olefins, 50% C4 paraffins, with a total flow of 1000kg/h.
Stream 3 produced in I (at a flow rate of 725kg/h and a C4-C8 olefin content of 225 kg/h) was fed to II, and 30% of stream 4 produced in II (at a flow rate of 197kg/h and an olefin content of greater than 95%) was returned to I.
The stream 2 obtained in I contains 64 kg/h of ethylene and 196g/h of propylene, the ethylene-propylene yield being 52.0% based on the effective feed (olefin) in stream 1.
The reaction materials entering I were stream 1 and stream 5, wherein stream 1 was 1000kg/h, stream 5 was 62kg/h, and the total amount was 1062kg/h.
[ example 5 ]
The procedure shown in fig. 1 was used:
stream 1 contains 45% C4 olefins, 3% C5 olefins, 2% C6 olefins, 50% C4 paraffins, and has a total flow of 1000kg/h.
Stream 3 produced in I (at a flow rate of 729kg/h and a C4-C8 olefin content of 229 kg/h) was fed to II and stream 4 produced in II (at a flow rate of 206kg/h and an olefin content of more than 95%) was returned to I in its entirety.
The stream 2 obtained in I contains 91 kg/h of ethylene and 273g/h of propylene, the ethylene-propylene yield being 72.8% based on the effective feed (olefin) in stream 1.
The reaction materials entering I were stream 1 and stream 5, wherein stream 1 was 1000kg/h, stream 5 was 206kg/h, and the total amount was 1206kg/h.
[ example 6 ]
The procedure shown in fig. 1 was used:
stream 1 contains 45% C4 olefins, 3% C5 olefins, 2% C6 olefins, 50% C4 paraffins, and has a total flow of 1000kg/h.
Stream 3 produced in I (having a flow rate of 728kg/h and a C4-C8 olefin content of 228 kg/h) was fed to II, and 90% of stream 4 produced in II (having a flow rate of 205kg/h and an olefin content of more than 95%) was returned to I.
The stream 2 obtained in I contains 87 kg/h of ethylene and 262g/h of propylene, the yield of ethylene and propylene being 69.8% based on the effective feed (olefin) in stream 1.
The reaction materials entering I were stream 1 and stream 5, wherein stream 1 was 1000kg/h, stream 5 was 185kg/h, and the total amount was 1185kg/h.
[ example 7 ]
The procedure shown in fig. 1 was used:
stream 1 contains 45% C4 olefins, 3% C5 olefins, 2% C6 olefins, 50% C4 paraffins, and has a total flow of 1000kg/h.
Stream 3 produced in I (at a flow rate of 726kg/h and a C4-C8 olefin content of 226 kg/h) was fed to II, and stream 4 produced in II (at a flow rate of 203kg/h and an olefin content of greater than 95%) was 70% returned to I.
The stream 2 obtained in I contains 80 kg/h of ethylene and 241g/h of propylene, the ethylene-propylene yield being 64.2% based on the effective feed (olefin) in stream 1.
The reaction materials entering I were stream 1 and stream 5, wherein stream 1 was 1000kg/h, stream 5 was 142kg/h, and the total amount was 1142kg/h.
[ example 8 ]
The procedure shown in fig. 1 was used:
stream 1 contains 45% C4 olefins, 3% C5 olefins, 2% C6 olefins, 50% C4 paraffins, and has a total flow of 1000kg/h.
Stream 3 produced in I (having a flow rate of 721kg/h and a C4-C8 olefin content of 221 kg/h) was fed to II, and 30% of stream 4 produced in II (having a flow rate of 199kg/h and an olefin content of greater than 95%) was returned to I.
The stream 2 obtained in I contains 66 kg/h of ethylene and 199g/h of propylene, the yield of ethylene and propylene being 53.0% based on the effective feed (olefin) in stream 1.
The reaction materials entering I are a stream 1 and a stream 5, wherein the flow rate of the stream 1 is 1000kg/h, the flow rate of the stream 5 is 60kg/h, and the total amount is 1060kg/h.
[ example 9 ]
The procedure shown in fig. 1 was used:
stream 1 contains 45% C4 olefins, 3% C5 olefins, 2% C6 olefins, 50% C4 paraffins, and has a total flow of 1000kg/h.
90% of stream 3 produced in I (having a flow rate of 728kg/h and a C4-C8 olefin content of 228 kg/h) is fed to II and stream 4 produced in II (having a flow rate of 185kg/h and an olefin content of more than 95%) is returned to I.
The stream 2 obtained in I contains 87 kg/h of ethylene and 262g/h of propylene, the yield of ethylene and propylene being 69.8% based on the effective feed (olefin) in stream 1.
The reaction materials entering I were stream 1 and stream 5, wherein stream 1 was 1000kg/h, stream 5 was 185kg/h, and the total amount was 1185kg/h.
[ example 10 ]
The procedure shown in fig. 1 was used:
stream 1 contains 45% C4 olefins, 3% C5 olefins, 2% C6 olefins, 50% C4 paraffins, and has a total flow of 1000kg/h.
70% of stream 3 produced in I (having a flow rate of 726kg/h and a C4-C8 olefin content of 226 kg/h) is fed to II and stream 4 produced in II (having a flow rate of 203kg/h and an olefin content of greater than 95%) is returned to I.
The stream 2 obtained in I contains 80 kg/h of ethylene and 241g/h of propylene, the ethylene-propylene yield being 64.2% based on the effective feed (olefin) in stream 1.
The reaction materials entering I were stream 1 and stream 5, wherein stream 1 was 1000kg/h, stream 5 was 142kg/h, and the total amount was 1142kg/h.
[ example 11 ]
The procedure shown in fig. 1 was used:
stream 1 contains 45% C4 olefins, 3% C5 olefins, 2% C6 olefins, 50% C4 paraffins, and has a total flow of 1000kg/h.
50% of stream 3 produced in I (having a flow rate of 723kg/h and a C4-C8 olefin content of 223 kg/h) is fed to II and stream 4 produced in II (having a flow rate of 101kg/h and an olefin content of greater than 95%) is returned to I.
The stream 2 obtained in I contains 73kg/h of ethylene and 219g/h of propylene, the yield of ethylene and propylene being 58.4% based on the effective feed (olefin) in stream 1.
The reaction materials entering I were stream 1 and stream 5, wherein the flow rate of stream 1 was 1000kg/h, the flow rate of stream 5 was 101kg/h, and the total amount was 1101kg/h.
[ example 12 ]
The procedure shown in fig. 1 was used:
stream 1 contains 45% C4 olefins, 3% C5 olefins, 2% C6 olefins, 50% C4 paraffins, and has a total flow of 1000kg/h.
30% of stream 3 produced in I (having a flow rate of 721kg/h and a C4-C8 olefin content of 221 kg/h) is fed to II and the whole of stream 4 produced in II (having a flow rate of 60kg/h and an olefin content of greater than 95%) is returned to I.
The stream 2 obtained in I contains 66 kg/h of ethylene and 199g/h of propylene, the yield of ethylene and propylene being 53% based on the available feed (olefin) in stream 1.
The reaction materials entering I are a stream 1 and a stream 5, wherein the flow rate of the stream 1 is 1000kg/h, the flow rate of the stream 5 is 60kg/h, and the total amount is 1060kg/h.
Comparative example 1
The procedure shown in fig. 2 was used:
stream 1 contains 45% C4 olefins, 3% C5 olefins, 2% C6 olefins, 50% C4 paraffins, and has a total flow of 1000kg/h.
86% of stream 3 produced in I (which had a flow rate of 3922kg/h and a C4-C8 olefin content of 349 kg/h) was returned to I.
The stream 2 obtained in I contains 90 kg/h of ethylene and 270g/h of propylene, the ethylene-propylene yield being 72.0% based on the effective feed (olefin) in stream 1.
The reaction materials entering I were stream 1 and stream 9, wherein stream 1 was 1000kg/h, stream 9 was 3373kg/h, and the total amount was 4373kg/h.
Compared with the examples 1 and 5, the comparative example has equivalent ethylene propylene yield, and the feeding amount of the reactor is increased by several times, thus greatly improving the energy consumption.
Comparative example 2
The procedure shown in fig. 2 was used:
stream 1 contains 45% C4 olefins, 3% C5 olefins, 2% C6 olefins, 50% C4 paraffins, and has a total flow of 1000kg/h.
50% of stream 3 produced in I (having a flow rate of 1279kg/h and a C4-C8 olefin content of 279 kg/h) is returned to I.
The stream 2 obtained in I contains 72 kg/h of ethylene and 216g/h of propylene, the ethylene-propylene yield being 57.6% based on the effective feed (olefin) in stream 1.
The reaction materials entering I were stream 1 and stream 9, wherein stream 1 was 1000kg/h, stream 9 was 639kg/h, and the total amount was 1639kg/h.
The list of embodiments is shown in Table 1.
TABLE 1
Claims (10)
1. A process for producing propylene and ethylene comprising the steps of:
(1) Feeding the hydrocarbon stream into an olefin cracking unit for reaction to obtain an ethylene-propylene-containing stream and an unreacted hydrocarbon stream;
(2) Feeding said unreacted hydrocarbon stream to an olefin polymerization unit;
(3) C produced by olefin laminating unit 8 + Recycling the components back to the olefin cracking unit;
the hydrocarbon stream comprises a hydrocarbon selected from C 4 ~C 8 At least one of the olefins; the hydrocarbon stream has an olefin content of no greater than 50% by weight of the hydrocarbon stream; at least 60% of the unreacted hydrocarbon stream in step (2) is fed to the olefin polymerization unit; c produced by olefin superposition units 8 + At least 30% of the components are recycled back to the olefin cracking unit;
the catalyst adopted by the olefin cracking unit contains ZSM-5 molecular sieve; the catalyst adopted by the olefin superposition unit is a solid phosphoric acid catalyst or a silicon-aluminum pellet catalyst.
2. The process for producing propylene and ethylene according to claim 1, wherein C is produced by a polymerization unit of olefins 8 + At least 70% of the components are recycled to the olefin cracking unit.
3. The process for producing propylene and ethylene according to claim 1, wherein C is produced by a polymerization unit of olefins 8 + At least 90% of the components are recycled to the olefin cracking unit.
4. The process for producing propylene and ethylene according to claim 1, characterized in that at least 100% of the unreacted hydrocarbon stream in step (2) is fed to the olefin polymerization unit.
5. The process for producing propylene and ethylene according to claim 1, characterized in that at least the reaction of olefin cracking into propylene and ethylene takes place in the olefin cracking unit.
6. The process for producing propylene and ethylene according to claim 1, wherein at least olefin double polymerization takes place in the olefin polymerization unit.
7. The process for producing propylene and ethylene according to claim 1, characterized in that the hydrocarbon stream contains a catalyst selected from the group consisting of C 4 ~C 6 At least one of the olefins.
8. The process for producing propylene and ethylene according to claim 1, characterized in that the hydrocarbon stream contains a catalyst selected from the group consisting of C 4 ~C 5 At least one of the olefins.
9. The process for producing propylene and ethylene as claimed in claim 1, wherein the hydrocarbon stream contains C 4 An olefin.
10. The process for producing propylene and ethylene according to claim 1, characterized in that in step (2) the hydrocarbon stream is fed to an olefin folding unit, obtaining an olefin-rich stream produced after olefin folding and an alkane-rich stream remaining after folding; the separation of the two streams is achieved by conventional separation.
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| CN201811275261.9A CN111116288B (en) | 2018-10-30 | 2018-10-30 | Method for producing propylene and ethylene |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2297301A1 (en) * | 2000-01-18 | 2001-07-18 | Uop Llc | Combination process for enhanced light olefin production |
| CN1642887A (en) * | 2002-03-15 | 2005-07-20 | 法国石油公司 | Multi-step method of converting a charge containing olefins with four, five or more carbon atoms in order to produce propylene |
| CN102531824A (en) * | 2011-12-29 | 2012-07-04 | 北京惠尔三吉绿色化学科技有限公司 | Process method for preparing propylene and ethylene from liquid gas including butylene |
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2018
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2297301A1 (en) * | 2000-01-18 | 2001-07-18 | Uop Llc | Combination process for enhanced light olefin production |
| CN1642887A (en) * | 2002-03-15 | 2005-07-20 | 法国石油公司 | Multi-step method of converting a charge containing olefins with four, five or more carbon atoms in order to produce propylene |
| CN102531824A (en) * | 2011-12-29 | 2012-07-04 | 北京惠尔三吉绿色化学科技有限公司 | Process method for preparing propylene and ethylene from liquid gas including butylene |
Non-Patent Citations (1)
| Title |
|---|
| 烯烃转化生产丙烯的研究进展;戴伟等;《石油化工》;20080515(第05期);425-433 * |
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